Reactor vessels with pressure and heat transfer features for producing hydrogen-based fuels and structural elements, and associated systems and methods

ABSTRACT

Reactor vessels with pressure and heat transfer features for producing hydrogen-based fuels and structural elements, and associated systems and methods. A representative reactor system includes a first reaction zone and a heat path, a reactant source coupled to the first reaction zone, and a first actuator coupled to cyclically pressurize the first reaction zone. A second reaction zone is in fluid communication with the first, a valve is coupled between the first and second reaction zones to control a flow rate therebetween, and a second actuator is coupled in fluid communication with the second reaction zone to cyclically pressurize the second reaction zone. First and second heat exchangers direct heat from products to reactants in the reaction zones. A controller controls the first and second actuators in a coordinated manner based at least in part on a flow rate of the second product from the second reaction zone.

CROSS-REFERENCE TO RELATED APPLICATIONS

The present application is a divisional of pending U.S. application Ser.No. 13/684,743 filed on Nov. 26, 2012 which is a continuation ofpatented U.S. application Ser. No. 13/027,060 filed Feb. 14, 2011, whichclaims priority to U.S. Provisional Application 61/304,403, filed Feb.13, 2010 and incorporated herein by reference. To the extent theforegoing provisional application and/or any other materialsincorporated herein by reference conflict with the present disclosure,the present disclosure controls.

TECHNICAL FIELD

The present technology relates generally to chemical reactor vesselswith pressure and heat transfer features for producing hydrogen-basedfuels and structural elements, and associated systems and methods. Inparticular embodiments, such reactor vessels can be used to produceclean-burning, hydrogen-based fuels from a wide variety of feedstocks,and can produce structural building blocks from carbon and/or otherelements that are released when forming the hydrogen-based fuels.

BACKGROUND

Renewable energy sources such as solar, wind, wave, falling water, andbiomass-based sources have tremendous potential as significant energysources, but currently suffer from a variety of problems that prohibitwidespread adoption. For example, using renewable energy sources in theproduction of electricity is dependent on the availability of thesources, which can be intermittent. Solar energy is limited by the sun'savailability (i.e., daytime only), wind energy is limited by thevariability of wind, falling water energy is limited by droughts, andbiomass energy is limited by seasonal variances, among other things. Asa result of these and other factors, much of the energy from renewablesources, captured or not captured, tends to be wasted.

The foregoing inefficiencies associated with capturing and saving energylimit the growth of renewable energy sources into viable energyproviders for many regions of the world, because they often lead to highcosts of producing energy. Thus, the world continues to rely on oil andother fossil fuels as major energy sources because, at least in part,government subsidies and other programs supporting technologydevelopments associated with fossil fuels make it deceptively convenientand seemingly inexpensive to use such fuels. At the same time, thereplacement cost for the expended resources, and the costs ofenvironment degradation, health impacts, and other by-products of fossilfuel use are not included in the purchase price of the energy resultingfrom these fuels.

In light of the foregoing and other drawbacks currently associated withsustainably producing renewable resources, there remains a need forimproving the efficiencies and commercial viabilities of producingproducts and fuels with such resources.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a partially schematic, partially cross-sectional illustrationof a solar-heated reactor vessel configured in accordance with anembodiment of the present technology.

FIG. 2 is a partially schematic, cross-sectional illustration of areactor having interacting endothermic and exothermic reaction zones inaccordance with an embodiment of the disclosure.

FIG. 3 is a flow diagram illustrating a chemical process having heattransfer characteristics and pressure variation characteristics inaccordance with an embodiment of the present technology.

DETAILED DESCRIPTION

1. Overview

Several examples of devices, systems and methods for conductinginterconnected exothermic and endothermic reactions in a chemicalreactor are described below. The interconnections can be based onpressure differences and/or temperature differences between regions andconstituents within the reactor. Such reactors can be used to producehydrogen fuels and/or other useful end products. Accordingly, thereactors can produce clean-burning fuel and can re-purpose carbon and/orother constituents for use in durable goods, including polymers andcarbon composites. Although the following description provides manyspecific details of the following examples in a manner sufficient toenable a person skilled in the relevant art to practice, make and usethem, several of the details and advantages described below may not benecessary to practice certain examples of the technology. Additionally,the technology may include other examples that are within the scope ofthe claims but are not described here in detail.

References throughout this specification to “one example,” “an example,”“one embodiment” or “an embodiment” mean that a particular feature,structure, process or characteristic described in connection with theexample is included in at least one example of the present technology.Thus, the occurrences of the phrases “in one example,” “in an example,”“one embodiment” or “an embodiment” in various places throughout thisspecification are not necessarily all referring to the same example.Furthermore, the particular features, structures, routines, steps orcharacteristics may be combined in any suitable manner in one or moreexamples of the technology. The headings provided herein are forconvenience only and are not intended to limit or interpret the scope ormeaning of the claimed technology.

Certain embodiments of the technology described below may take the formof computer-executable instructions, including routines executed by aprogrammable computer or controller. Those skilled in the relevant artwill appreciate that the technology can be practiced on computer orcontroller systems other than those shown and described below. Thetechnology can be embodied in a special-purpose computer, controller, ordata processor that is specifically programmed, configured orconstructed to perform one or more of the computer-executableinstructions described below. Accordingly, the terms “computer” and“controller” as generally used herein refer to any data processor andcan include internet appliances, hand-held devices, multi-processorsystems, programmable consumer electronics, network computers,mini-computers, and the like. The technology can also be practiced indistributed environments where tasks or modules are performed by remoteprocessing devices that are linked through a communications network.Aspects of the technology described below may be stored or distributedon computer-readable media, including magnetic or optically readable orremovable computer discs as well as media distributed electronicallyover networks. In particular embodiments, data structures andtransmissions of data particular to aspects of the technology are alsoencompassed within the scope of the present technology. The presenttechnology encompasses both methods of programming computer-readablemedia to perform particular steps, as well as executing the steps.

2. Representative Reactors and Associated Methodologies

FIG. 1 is a partially schematic, partially cross-sectional illustrationof a system 100 configured to conduct interactive endothermic andexothermic chemical reactions in accordance with an embodiment of thepresent technology. The system 100 can include a reactor vessel 101having multiple reaction zones, shown in FIG. 1 as a first reaction zone110 and a second reaction zone 120. The system 100 includes features forproviding energy to both reaction zones, for example, a suitable heatsource, such as a solar concentrator 103 positioned to direct solarenergy 106 into the first reaction zone 110. In this embodiment, thereactor vessel 101 and the solar concentrator 103 are mounted to apedestal 102 that can move with multiple degrees of freedom (e.g. rotateabout two orthogonal axes) to position the solar concentrator 103 tocapture solar energy throughout the course of the day.

The system 100 can further include supplies of reactants and otherchemical constituents, including a methane supply 153 a, a carbondioxide supply 153 b, and a hydrogen supply 154. In a particularembodiment, the methane and carbon dioxide are provided to the reactorvessel 101 to produce methanol. The methanol represents a denser and/ormore versatile hydrogen carrier that has increased utility for vehicleand other fuel storage and transport purposes. The hydrogen can bestored at a hydrogen storage tank 108. As will be described in furtherdetail below, the hydrogen can be used to pressurize the second reactionzone 120, and/or provide power to an engine 104 and generator 105. Thegenerator 105 can provide power for the overall system 100. In otherembodiments, the engine 104 and/or generator 105 can be located far awayfrom the rest of the system 100 and can provide power to devices otherthan the system 100. In such cases, the hydrogen can be supplied to theengine 104 via a pipeline or other transport device. The system 100 canfurther include features that allow the reactions at the first andsecond reaction zones 110, 120 to continue in the absence of sufficientsolar energy (e.g. at night). Further details are described below withreference to FIG. 2. The system 100 can also include a controller 190that receives input signals 191 from any of a variety of sensors,transducers, and/or other elements of the system 100, and, in responseto information received from these elements, delivers control signals192 to adjust operational parameters of the system 100. Further detailsof representative closed-loop control arrangements are also describedfurther below with reference to FIGS. 2 and 3.

FIG. 2 is a partially schematic, cross-sectional illustration ofparticular components of the system 100, including the reactor vessel101. The reactor vessel 101 includes the first reaction zone 110positioned toward the upper left of FIG. 2 (e.g., at a first reactorportion) to receive incident solar radiation 106, e.g., through a solartransmissive surface 107. The second reaction zone 120 is alsopositioned within the reactor vessel 101, e.g., at a second reactorportion, to receive products from the first reaction zone 110 and toproduce an end product, for example, methanol. Reactant sources 153provide reactants to the reactor vessel 101, and a product collector 123collects the resulting end product. A regulation system 150, which caninclude valves 151 or other regulators and corresponding actuators 152,is coupled to the reactant sources 153 to control the delivery ofreactants to the first reaction zone 110 and to control other flowswithin the system 100. In other embodiments, the valves can be replacedby or supplemented with other mechanisms, e.g., pumps.

In a particular embodiment, the reactant sources 153 include a methanesource 153 a and a carbon dioxide source 153 b. The methane source 153 ais coupled to a first reactant valve 151 a having a correspondingactuator 152 a, and the carbon dioxide source 153 b is coupled to asecond reactant valve 151 b having a corresponding actuator 152 b. Thereactants pass into the reaction vessel 101 and are conducted upwardlyaround the second reaction zone 120 and the first reaction zone 110 asindicated by arrows A. As the reactants travel through the reactorvessel 101, they can receive heat from the first and second reactionzones 110, 120 and from products passing from the first reaction zone110 to the second reaction zone 120, as will be described in furtherdetail later. The reactants enter the first reaction zone 110 at a firstreactant port 111. At the first reaction zone 110, the reactants canundergo the following reaction:CH₄+C0₂+HEAT−2CO+2H₂  [Equation 1]

In a particular embodiment, the foregoing endothermic reaction isconducted at about 900° C. and at pressures of up to about 1,500 psi. Inother embodiments, reactions with other reactants can be conducted atother temperatures at the first reaction zone 110. The first reactionzone 110 can include any of a variety of suitable catalysts, forexample, a nickel/aluminum oxide catalyst. In particular embodiments thereactants and/or the first reaction zone 110 can be subjected toacoustic pressure fluctuation (in addition to the overall pressurechanges caused by introducing reactants, undergoing the reaction, andremoving products from the first reaction zone 110) to aid in deliveringthe reactants to the reaction sites of the catalyst. In any of theseembodiments, the products produced at the first reaction zone 110 (e.g.carbon monoxide and hydrogen) exit the first reaction zone 110 at afirst product port 112 and enter a first heat exchanger 140 a. The firstproducts travel through the first heat exchanger 140 a along a firstflow path 141 and transfer heat to the incoming reactants travelingalong a second flow path 142. Accordingly, the incoming reactants can bepreheated at the first heat exchanger 140 a, and by virtue of passingalong or around the outside of the first reaction zone 110. Inparticular embodiments, one or more surfaces of the first heat exchanger140 a can include elements or materials that absorb radiation at onefrequency and re-radiate it at another. Further details of suitablematerials and arrangements are disclosed in co-pending U.S. applicationSer. No. 13/027,015 titled CHEMICAL REACTORS WITH RE-RADIATING SURFACESAND ASSOCIATED SYSTEMS AND METHODS, filed concurrently herewith andincorporated herein by reference.

The first products enter the second reaction zone 120 via a secondreactant port 121 and a check valve 156 or other flow inhibitor. Thecheck valve 156 is configured to allow a one-way flow of the firstproducts into the second reaction zone 120 when the pressure of thefirst products exceeds the pressure in the second reaction zone 120. Inother embodiments, the check valve 156 can be replaced with anothermechanism, e.g., a piston or pump that conveys the first products to thesecond reaction zone 120.

At the second reaction zone 120, the first products from the firstreaction zone 110 undergo an exothermic reaction, for example:2CO+2H₂+2′H₂→CH₃OH+HEAT  [Equation 2]

The foregoing exothermic reaction can be conducted at a temperature ofapproximately 250° C. and in many cases at a pressure higher than thatof the endothermic reaction in the first reaction zone 110. To increasethe pressure at the second reaction zone 120, the system 100 can includean additional constituent source 154 (e.g. a source of hydrogen) that isprovided to the second reaction zone 120 via a valve 151 c andcorresponding actuator 152 c. The additional constituent (e.g. hydrogen,represented by 2′H2 in Equation 2) can pressurize the second reactionzone with or without necessarily participating as a consumable in thereaction identified in Equation 2. In particular, the additionalhydrogen may be produced at pressure levels beyond 1,500 psi, e.g., upto about 5,000 psi or more, to provide the increased pressure at thesecond reaction zone 120. In a representative embodiment, the additionalhydrogen may be provided in a separate dissociation reaction usingmethane or another reactant. For example, the hydrogen can be producedin a separate endothermic reaction, independent of the reactions at thefirst and second reaction zones 110, 120, as follows:CH₄+HEAT→C+2H₂  [Equation 3]

In addition to producing hydrogen for pressurizing the second reactionzone 120, the foregoing reaction can produce carbon suitable to serve asa building block in the production of any of a variety of suitable endproducts, including polymers, self-organizing carbon-based structuressuch as graphene, carbon composites, and/or other materials. Furtherexamples of suitable products are included in co-pending U.S.application Ser. No. 13/027,214, now U.S. Pat. No. 8,980,416, titledARCHITECTURAL CONSTRUCT HAVING FOR EXAMPLE A PLURALITY OF ARCHITECTURALCRYSTALS, filed Feb. 14, 2011 concurrently herewith and incorporatedherein by reference.

The reaction at the second reaction zone 120 can be facilitated with asuitable catalyst, for example, copper, zinc, aluminum and/or compoundsincluding one or more of the foregoing elements. The product resultingfrom the reaction at the second reaction zone 120 (e.g. methanol) iscollected at the product collector 123. Accordingly, the methanol exitsthe second reaction zone 120 at a second product port 122 and passesthrough a second heat exchanger 140 b. At the second heat exchanger 140b, the methanol travels along a third flow path 143 and transfers heatto the incoming constituents provided to the first reaction zone 110along a fourth flow path 144. Accordingly, the two heat exchangers 140a, 140 b can increase the overall efficiency of the reactions takingplace in the reactor vessel 101 by conserving and recycling the heatgenerated at the first and second reaction zones.

In a particular embodiment, energy is provided to the first reactionzone 110 via the solar concentrator 103 described above with referenceto FIG. 2. Accordingly, the energy provided to the first reaction zone110 by the solar collector 103 will be intermittent. The system 100 caninclude a supplemental energy source that allows the reactions tocontinue in the absence of sufficient solar energy. In particular, thesystem 100 can include a supplemental heat source 155. For example, thesupplemental heat source 155 can include a combustion reactant source155 a (e.g. providing carbon monoxide) and an oxidizer source 155 b(e.g. providing oxygen). The flows from the reactant source 155 a andoxidizer source 155 b are controlled by corresponding valves 151 d, 151e, and actuators 152 d, 152 e. In operation, the reactant and oxidizerare delivered to the reactor vessel 101 via corresponding conduits 157a, 157 b. The reactant and oxidizer can be preheated within the reactorvessel 101, before reaching a combustion zone 130, as indicated by arrowB. At the combustion zone 130, the combustion reactant and oxidizer arecombusted to provide heat to the first reaction zone 110, thussupporting the endothermic reaction taking place within the firstreaction zone 110 in the absence of sufficient solar energy. The resultof the combustion can also yield carbon dioxide, thus reducing the needfor carbon dioxide from the carbon dioxide source 153 b. The controller190 can control when the secondary heat source 155 is activated anddeactivated, e.g., in response to a heat or light sensor.

In another embodiment, the oxygen provided by the oxidizer source 155 bcan react directly with the methane at the combustion zone 130 toproduce carbon dioxide and hydrogen. This in turn can also reduce theamount of carbon dioxide required at the first reaction zone 110.

As noted above, Equation 1 represents an endothermic reaction, andEquation 2 represents an exothermic reaction. In addition, the forwardprogress of Equation 1 is supported by a relatively low pressureenvironment, while the forward progress of Equation 2 is supported by arelatively high pressure environment. The present technology includescontrolling the heats and pressures produced and required in the tworeaction zones in an inter-dependent manner to enhance (e.g. optimize)the production rate of methanol or other end products. FIG. 3 identifiesthe general manner in which this is accomplished, and the details ofparticular embodiments are then further described. Referring now toFIGS. 2 and 3, an overall process 300 that can be conducted with thesystem 100 described above includes directing reactants, including ahydrogenous compound, to a first reaction zone 110 (process portion301). For example, the hydrogenous compound can include the methanedescribed above. In other embodiments, the hydrogenous compound caninclude other hydrocarbons, or other hydrogen-bearing compounds that donot necessarily include carbon (e.g. nitrogenous compounds). In processportion 302, the pressure at the first reaction zone 110 is cyclicallyvaried in accordance with a first cycle. For example, the pressure inthe first reaction zone 110 can be adjusted by adjusting the pressureand/or flow rate with which reactants are directed into the firstreaction zone 110, and by the rate at which the resulting products leavethe first reaction zone 110. Process portion 303 includes directing heatinto the first reaction zone to heat the reactants. The heat added tothe first reaction zone 110 also increases the pressure in the firstreaction zone 110 and accordingly represents an additional pressurecontrol variable. Process portion 304 includes dissociating thehydrogenous compound to produce the first products in the endothermicreaction. In a representative embodiment, the endothermic reactionincludes the reaction described above with reference to Equation 1, andin other embodiments, the reaction can include different products and/orreactants, while still absorbing heat.

In process portion 305, the first products are transferred to the secondreaction zone 120, while transferring heat from the first products toreactants in transit to the first reaction zone 110. For example, theforegoing heat transfer process can be conducted by the first heatexchanger 140 a described above with reference to FIG. 2. In processportion 306, the pressure at the second reaction zone 120 is cyclicallyvaried in accordance with a second cycle. For example, the pressure inthe second reaction zone 120 can be adjusted by adjusting the flow offirst products into the second reaction zone 120, and by adjusting theflow of hydrogen (or another additional constituent) from the additionalconstituent source 154 into the second reaction zone 120. Processportion 307 includes producing second products at the second reactionzone 120, including at least one of a hydrogen-based fuel and astructural building block, in an exothermic reaction. For example,Equation 2 above includes forming methanol at the second reaction zone120. In other embodiments, other processes can be conducted at thesecond reaction zone 120 to produce other hydrogen-based fuels. In stillfurther embodiments, the resulting products can include structuralbuilding blocks, e.g., building blocks formed from carbon, boron,nitrogen, or other elements. Representative reactants, products andprocesses are described in further detail in the following co-pendingU.S. applications, filed Feb. 14, 2011 and incorporated herein byreference: application Ser. No. 13/027,208, now U.S. Pat. No. 8,318,131,titled CHEMICAL PROCESSES AND REACTORS FOR EFFICIENTLY PRODUCINGHYDROGEN FUELS AND STRUCTURAL MATERIALS, AND ASSOCIATED SYSTEMS ANDMETHODS; application Ser. No. 13/027,068, now U.S. Pat. No. 8,318,997,titled CARBON-BASED DURABLE GOODS AND RENEWABLE FUEL FROM BIOMASS WASTEDISSOCIATION; and application Ser. No. 13/027,214, now U.S. Pat. No.8,980,416, titled ARCHITECTURAL CONSTRUCT HAVING FOR EXAMPLE A PLURALITYOF ARCHITECTURAL CRYSTALS. Process portion 308 includes transferringheat from the second products to the reactants in transit to the firstreaction zone, e.g. via the second heat exchanger 140 b described abovewith reference to FIG. 2.

The detailed steps outlined below identify the operation of the system100 in accordance with a further particular embodiment:

-   -   1. Provide methane and carbon dioxide to the first reaction zone        110 under pressure. In a representative embodiment, the pressure        in the first reaction zone 110 cycles between about 50 psi and        about 1500 psi.    -   2. Elevate the temperature in the first reaction zone 110,        causing an endothermic reaction to proceed.    -   3. Produce hydrogen and carbon monoxide (first products) at the        first reaction zone 110. As the hydrogen and carbon monoxide are        produced, the pressure in the first reaction zone 110 increases,        which slows the reaction rate. As the reaction rate slows, the        first reaction zone 110 continues to heat.    -   4. As the pressure in the first reaction zone 110 exceeds the        pressure in the second reaction zone 120, direct the hydrogen        and carbon monoxide to flow to second reaction zone 120. This        will reduce the pressure in the first reaction zone 110.    -   5. As the carbon monoxide and hydrogen pass to the second        reaction zone 120, transfer heat from these constituents to the        methane and carbon dioxide flowing to the first reaction zone        110.    -   6. As the pressure decreases in the first reaction zone 110, the        endothermic reaction rate there increases, as does the rate at        which the hydrogen and carbon monoxide are delivered to the        second reaction zone 120. This will increase the pressure in the        second reaction zone 120.    -   7. Further pressurize the second reaction zone 120 with a        separate source of hydrogen, e.g., provided in quantities that        may exceed a stoichiometric balance.    -   8. The pressure in the second reaction zone 120 increases to the        point that hydrogen and carbon monoxide from the first reaction        zone 110 no longer enter the second reaction zone 120.    -   9. At the second reaction zone 120, combine carbon monoxide and        hydrogen to produce methanol. The rate of this exothermic        reaction increases with pressure.    -   10. Provide occasional release of the methanol from the second        reaction zone 120, thus reducing the pressure there to        reactivate the reaction bed. Releasing the pressure decreases        the reaction rate. The pressure at the second reaction zone 120        can generally be at a higher pressure, but can accordingly cycle        between a low valve of, e.g., about 50 psi, and a high valve of,        e.g., about 5,000 psi or more.    -   11. Transfer heat from the methanol exiting the second reaction        zone 120 to the methane and carbon dioxide flowing to the first        reaction zone 110.    -   12. As the pressure in the second reaction zone 120 falls below        the pressure in the first reaction zone 110, return to step 4.    -   13. Control the pressures in the first and second reaction zones        110, 120 to enhance (e.g., maximize) the production of methanol.

One feature of embodiments of the systems and processes described abovewith reference to FIG. 1-3 is that they include internally transferringheat between chemical constituents participating in the reactions. Anadvantage of this arrangement is that it reduces overall heat losses byrecycling the heat produced and required in the exothermic andendothermic reactions, thus increasing the overall thermodynamicefficiency of the process. This in turn is expected to reduce the costof producing high-quality, clean-burning hydrogen-based fuels and/or thebuilding block constituents (e.g., carbon) that can be re-purposed toproduce durable goods. Such goods represent an additional revenue streamthat can in turn reduce the cost to produce the hydrogen-based fuel.

Another feature of at least some of the foregoing embodiments is thatthe pressures and flow rates of the constituents involved in theendothermic and exothermic reactions can be controlled to take advantageof reaction rates that are favored by high pressures and by lowpressures. By coupling the flows of constituents in a manner thatreflects the pressure differentials and temperature differentialsbetween the reactions, the overall rate of production of the end product(e.g., methanol in a particular example) can be enhanced (e.g.,optimized and/or maximized). This process can be performed automaticallyor autonomously by the controller 190 described above, based on sensedvalues throughout the system to provide real-time control of the productproduction.

From the foregoing, it will appreciated that specific embodiments of thetechnology have been described herein for purposes of illustration, butthat various modifications may be made without deviating from thetechnology. For example, in addition to adjusting the foregoingparameters to efficiently utilize the available solar energy, theparameters can be adjusted to account for varying rates of solar energy,and/or to maximize the life of the catalysts in the first reaction zone110 and/or the second reaction zone 120. While embodiments werediscussed above in the context of a particular hydrocarbon (e.g.,methane), other hydrocarbons (e.g., gasoline, propane, butane, dieselfuel, kerosene, bunker fuel and/or others) can also be suitable. Inother embodiments, the reactants can include other carbon-based hydrogendonors, or hydrogen-containing compounds that include elements otherthan carbon. For example, the process can include extracting nitrogenfrom air or another source, and combining the nitrogen with hydrogen toproduce ammonia. In still further embodiments, the system can operatewithout cyclically varying the pressure in the first and/or secondreaction zones. For example, the first reaction zone can run at arelatively low pressure and the second reaction zone can run at arelatively high pressure. In such cases, a pump, piston or other devicecan add work to the first products to direct them to the second reactionzone. In a further aspect of such cases, ultrasonic energy at the firstand/or second reaction zones can be used to load reactants and removeproducts.

A variety of sources can be used to produce suitable inputs for thereactor. For example, carbohydrates and carbon dioxide produced bybreweries, bakeries, power plants, coking and/or calcining operationsand/or others can be supplied to the reactor. In any of theseembodiments, one feature of the processes is to increase the density ofthe hydrogen, for example, to the point where the hydrogen can be storedin existing fuel tanks currently used for conventional fuels. Othersuitable products that may be formed with carbon extracted during theforegoing processes can include diamond-like platings, e.g., forfriction reduction, increased thermal conductivity and/or opticalpurposes, graphene crystal formation, macroscopic fibers, scrolls andother shapes, colorants and additives for polymers, and/or dopedsemiconductor materials.

Certain aspects of the technology described in the context of particularembodiments may be combined or eliminated in other embodiments. Forexample, multiple reactors of the type shown in FIG. 2 can producedifferent products that serve as reactants for each other. The specificdetails of the reactor described above in the context of FIG. 2, and thesteps enumerated above can be eliminated or changed in otherembodiments. Further, while advantages associated with certainembodiments of the technology have been described in the context ofthose embodiments, other embodiments may also exhibit such advantages,and not all embodiments need necessarily exhibit such advantages to fallwithin the scope of the present disclosure. Accordingly, the presentdisclosure and associated technology can encompass other embodiments notexpressly shown or described herein.

To the extent not previously incorporated herein by reference, thepresent application incorporates by reference in their entirety thesubject matter of each of the following materials: U.S. patentapplication Ser. No. 12/857,553, now U.S. Pat. No. 8,940,265, filed onAug. 16, 2010 and titled SUSTAINABLE ECONOMIC DEVELOPMENT THROUGHINTEGRATED PRODUCTION OF RENEWABLE ENERGY, MATERIALS RESOURCES, ANDNUTRIENT REGIMES; U.S. patent application Ser. No. 12/857,541, now U.S.Pat. No. 9,231,267, filed on Aug. 16, 2010 and titled SYSTEMS ANDMETHODS FOR SUSTAINABLE ECONOMIC DEVELOPMENT THROUGH INTEGRATED FULLSPECTRUM PRODUCTION OF RENEWABLE ENERGY; U.S. patent application Ser.No. 12/857,554, now U.S. Pat. No. 8,808,529, filed on Aug. 16, 2010 andtitled SYSTEMS AND METHODS FOR SUSTAINABLE ECONOMIC DEVELOPMENT THROUGHINTEGRATED FULL SPECTRUM PRODUCTION OF RENEWABLE MATERIAL RESOURCESUSING SOLAR THERMAL; U.S. patent application Ser. No. 12/857,502, nowU.S. Pat. No. 9,097,152, filed on Aug. 16, 2010 and titled ENERGY SYSTEMFOR DWELLING SUPPORT; U.S. patent application Ser. No. 13/027,235, filedon Feb. 14, 2011, now U.S. Pat. No. 8,313,556 and titled DELIVERYSYSTEMS WITH IN-LINE SELECTIVE EXTRACTION DEVICES AND ASSOCIATED METHODSOF OPERATION; U.S. Patent Application No. 61/401,699, filed on Aug. 16,2010 and titled COMPREHENSIVE COST MODELING OF AUTOGENOUS SYSTEMS ANDPROCESSES FOR THE PRODUCTION OF ENERGY, MATERIAL RESOURCES AND NUTRIENTREGIMES; U.S. patent application Ser. No. 13/027,208 filed on Feb. 14,2011, now U.S. Pat. No. 8,318,131 and titled CHEMICAL PROCESSES ANDREACTORS FOR EFFICIENTLY PRODUCING HYDROGEN FUELS AND STRUCTURALMATERIALS, AND ASSOCIATED SYSTEMS AND METHODS; U.S. patent applicationSer. No. 13/026,996, now U.S. Pat. No. 9,206,045, filed on Feb. 14, 2011and titled REACTOR VESSELS WITH TRANSMISSIVE SURFACES FOR PRODUCINGHYDROGEN-BASED FUELS AND STRUCTURAL ELEMENTS, AND ASSOCIATED SYSTEMS ANDMETHODS; U.S. patent application Ser. No. 13/027,015 filed on Feb. 14,2011 and titled CHEMICAL REACTORS WITH RE-RADIATING SURFACES ANDASSOCIATED SYSTEMS AND METHODS; U.S. application Ser. No. 13/027,244filed on Feb. 14, 2011 and titled THERMAL TRANSFER DEVICE AND ASSOCIATEDSYSTEMS AND METHODS; U.S. patent application Ser. No. 13/026,990 filedon Feb. 14, 2011, now U.S. Pat. No. 8,187,549 and titled CHEMICALREACTORS WITH ANNULARLY POSITIONED DELIVERY AND REMOVAL DEVICES, ANDASSOCIATED SYSTEMS AND METHODS; U.S. patent application Ser. No.13/027,181 filed on Feb. 14, 2011, now U.S. Pat. No. 8,187,550 andtitled REACTORS FOR CONDUCTING THERMOCHEMICAL PROCESSES WITH SOLAR HEATINPUT, AND ASSOCIATED SYSTEMS AND METHODS; U.S. patent application Ser.No. 13/027,215 filed on Feb. 14, 2011, now U.S. Pat. No. 8,318,269 andtitled INDUCTION FOR THERMOCHEMICAL PROCESS, AND ASSOCIATED SYSTEMS ANDMETHODS; U.S. patent application Ser. No. 13/027,198, now U.S. Pat. No.9,188,086, filed on Feb. 14, 2011 and titled COUPLED THERMOCHEMICALREACTORS AND ENGINES, AND ASSOCIATED SYSTEMS AND METHODS; U.S. PatentApplication No. 61/385,508, filed on Sep. 22, 2010 and titled REDUCINGAND HARVESTING DRAG ENERGY ON MOBILE ENGINES USING THERMAL CHEMICALREGENERATION; U.S. patent application Ser. No. 13/027,214, now U.S. Pat.No. 8,980,416, filed on Feb. 14, 2011 and titled ARCHITECTURAL CONSTRUCTHAVING FOR EXAMPLE A PLURALITY OF ARCHITECTURAL CRYSTALS; U.S. patentapplication Ser. No. 12/806,634, now U.S. Pat. No. 8,441,361, filed onAug. 16, 2010 and titled METHODS AND APPARATUSES FOR DETECTION OFPROPERTIES OF FLUID CONVEYANCE SYSTEMS; U.S. patent application Ser. No.13/027,188 filed on Feb. 14, 2011, now U.S. Pat. No. 8,312,759 andtitled METHODS, DEVICES, AND SYSTEMS FOR DETECTING PROPERTIES OF TARGETSAMPLES; U.S. patent application Ser. No. 13/027,068 filed on Feb. 14,2011, now U.S. Pat. No. 8,318,997 titled SYSTEM FOR PROCESSING BIOMASSINTO HYDROCARBONS, ALCOHOL VAPORS, HYDROGEN, CARBON, ETC.; U.S. patentapplication Ser. No. 13/027,196, now U.S. Pat. No. 8,912,239, filed onFeb. 14, 2011 and titled CARBON RECYCLING AND REINVESTMENT USINGTHERMOCHEMICAL REGENERATION; U.S. patent application Ser. No. 13/027,195filed on Feb. 14, 2011, now U.S. Pat. No. 8,784,095 and titledOXYGENATED FUEL; U.S. Patent Application No. 61/237,419, filed on Aug.27, 2009 and titled CARBON SEQUESTRATION; U.S. Patent Application No.61/237,425, filed on Aug. 27, 2009 and titled OXYGENATED FUELPRODUCTION; U.S. patent application Ser. No. 13/027,197 filed on Feb.14, 2011, now U.S. Pat. No. 8,070,835 and titled MULTI-PURPOSE RENEWABLEFUEL FOR ISOLATING CONTAMINANTS AND STORING ENERGY; U.S. PatentApplication No. 61/421,189, filed on Dec. 8, 2010 and titled LIQUIDFUELS FROM HYDROGEN, OXIDES OF CARBON, AND/OR NITROGEN; AND PRODUCTIONOF CARBON FOR MANUFACTURING DURABLE GOODS; U.S. patent application Ser.No. 13/027,185 filed on Feb. 14, 2011, now U.S. Pat. No. 8,328,888 andtitled ENGINEERED FUEL STORAGE, RESPECIATION AND TRANSPORT.

I claim:
 1. A method for processing a hydrogenous compound, comprising:directing reactants, including a hydrogenous compound, to a firstreaction zone; cyclically varying a pressure at the first reaction zonein accordance with a first cycle; directing heat into the first reactionzone to heat the reactants; dissociating the hydrogenous compound toproduce a first product in an endothermic reaction; transferring thefirst product to a second reaction zone; cyclically varying a pressureat the second reaction zone in accordance with a second cycle; at thesecond reaction zone, producing a second product including at least oneof a hydrogen-based fuel and a structural building block in anexothermic reaction; controlling a flow rate between the first andsecond reaction zones with a mechanism coupled between the first andsecond reaction zones; and controlling the pressure in the secondreaction zone based at least in part on a flow rate of the first productfrom the first reaction zone to the second reaction zone.
 2. The methodof claim 1 wherein cyclically varying the pressure at the first reachingzone is performed in response to a rate at which the second product isproduced at the second reaction zone.
 3. The method of claim 1, furthercomprising: at first pressure portions of the first cycle, increasing arate at which heat is collected at the first reaction zone; and atsecond pressure portions of the first cycle, increasing a rate of theendothermic reaction, the second pressure portions being lower than thefirst pressure portions.
 4. The method of claim 1, further comprising:at first pressure portions of the second cycle, increasing a rate of theexothermic reaction; and at second pressure portions of the secondcycle, increasing a rate at which the dissociation products aretransferred to the second reaction zone, the second pressure portionsbeing lower than the first pressure portions.
 5. The method of claim 1wherein directing reactants includes directing methane and carbondioxide.
 6. The method of claim 1 wherein producing first productsincludes producing hydrogen and carbon monoxide.
 7. The method of claim1 wherein directing heat includes directing solar radiation.
 8. Themethod of claim 7 wherein directing solar radiation includes directingsolar radiation during daylight hours and wherein directing heatincludes directing heat other than solar radiation at other thandaylight hours.
 9. The method of claim 1 wherein cyclically varying apressure at the second reaction zone includes directing an additionalamount of a consultant present in the first products.
 10. The method ofclaim 9 wherein directing an additional amount of the constituentincludes directing an additional amount of the constituent beyond anamount sufficient to stoichiometrically balance the exothermic reaction.11. The method of claim 1, further comprising controlling a rate of theendothermic reaction by controlling a pressure in the first reactionzone.
 12. The method of claim 1, further comprising controlling thepressures in the first and second reaction zones in a coordinated mannerbased at least in part on a rate at which the second product is producedat the second reaction zone.
 13. The method of claim 1, whereindirecting reactants includes directing methane and carbon dioxide to thefirst reaction zone under a controlled pressure and wherein the methodfurther comprises: (a) elevating a temperature in the first reactionzone to further increase the pressure at the first reaction zone; (b)dissociating the methane in the endothermic reaction at the firstreaction zone to produce hydrogen and carbon monoxide; (c) as thepressure in the first reaction zone exceeds a pressure in a secondreaction zone, directing the hydrogen and carbon monoxide to flow to thesecond reaction zone, causing the pressure in the first reaction zone todecrease and the reaction rate at the first reaction zone to increase,and causing the pressure in the second reaction zone to increase; (d)transferring heat from (1) the carbon monoxide and hydrogen passing tothe second reaction zone to (2) methane and carbon dioxide flowing tothe first reaction zone; (e) further pressurizing the second reactionzone with additional hydrogen not received from the first reaction zone;(f) causing the pressure in the second reaction zone to increase abovethe pressure in the first reaction zone to preclude hydrogen and carbonmonoxide in the first reaction zone from entering the second reactionzone; (g) at the second reaction zone, combining carbon monoxide andhydrogen to produce methanol in an exothermic reaction that increases inrate as a function of increasing pressure; (h) releasing the methanolfrom the second reaction zone to reduce the pressure and reaction at thesecond reaction zone; (i) transferring heat from the methanol exitingthe second reaction zone to methane and carbon dioxide flowing to thefirst reaction zone; and (j) as the pressure in the second reaction zonefalls below the pressure in the first reaction zone, repeating processes(c)-(j); and wherein cyclically varying the pressures in the first andsecond reaction zones is based at least in part on a rate at whichmethanol is released from the second reaction zone.
 14. The method ofclaim 13 further comprising forming the additional hydrogen bydissociating hydrogen from methane in a reaction separate from theendothermic reaction in the first reaction zone.
 15. The method of claim13 wherein directing solar radiation is performed during daylight hours,and wherein the method further comprises directing heat from other solarradiation to the first reaction zone during non-daylight hours.
 16. Themethod of claim 15 wherein directing heat includes oxidizing carbonmonoxide.
 17. The method of claim 13 further comprising conducting theendothermic reaction at the first reaction zone in the presence of anickel alumina catalyst.
 18. The method of claim 13 wherein performingthe endothermic reaction includes performing the endothermic reaction ata temperature of about 900.degree. C. and a pressure of up to about 155psi.
 19. The method of claim 13 wherein performing the exothermicreaction includes performing the exothermic reaction at a temperature ofabout 250.degree. C. and a pressure of up to about 5000 psi.